Multi-tubular chemical reactor with igniter for initiation of gas phase exothermic reactions

ABSTRACT

A multi-tubular chemical reactor includes an igniter for the initiation of gas phase exothermic reaction within the gas phase reaction zones of the tubular reactor units. In accordance with the present disclosure, there is provided a multi-tubular chemical reactor comprising a plurality of spaced-apart reactor units, each reactor unit comprising an elongate tube having a wall with internal and external surfaces, an inlet at one end and an outlet at the opposing end, the wall enclosing a gaseous flow passageway at least a portion of which defines a gas phase reaction zone, the multi-tubular chemical reactor can include at least one igniter for initiation of at least one gas phase exothermic reaction within a gas phase reaction zone of a reactor unit.

The present application is a U.S. National Phase Application of PCT International Application No. PCT/US2019/048822, filed on Aug. 29, 2019, to which priority is claimed, the entire contents of which are incorporated by reference herein.

CROSS REFERENCE TO RELATED APPLICATION

This application relates to subject matter disclosed and claimed in U.S. patent application Ser. Nos. 61/900,510 and 61/900,543, both filed on Nov. 6, 2013, the entire contents of which are incorporated by reference herein.

BACKGROUND OF THE INVENTION

The present disclosure relates to chemical reactors and, more particularly, to multi-tubular chemical reactors incorporating igniters for initiation of multiple gas phase exothermic reactions therein.

The teachings of the present disclosure, while generally applicable to multi-tubular reactors of all types for conducting all manner of gas phase exothermic reactions, will be specifically exemplified herein by multi-tubular reformers and methods of operating such reformers to bring about the gas phase exothermic reforming of liquid and gaseous reformable fuels to produce hydrogen-rich reformates.

The conversion of a gaseous or vaporized liquid reformable fuel to a hydrogen-rich carbon monoxide-containing gas mixture, a product commonly referred to as “synthesis gas” or “syngas,” can be carried out in accordance with any of such well known gas phase fuel reforming operations as steam reforming, dry reforming, autothermal reforming and catalytic partial oxidation (CPOX) reforming. Each of these fuel reforming operations has its distinctive chemistry and requirements and each is marked by its advantages and disadvantages relative to the others.

The development of improved fuel reformers, fuel reformer components, and reforming processes continues to be the focus of considerable research due to the potential of fuel cells, i.e., devices for the electrochemical conversion of electrochemically oxidizable fuels such as hydrogen, mixtures of hydrogen and carbon monoxide, and the like, to electricity, to play a greatly expanded role for general applications including main power units (MPUs) and auxiliary power units (APUs). Fuel cells also can be used for specialized applications, for example, as on-board electrical generating devices for electric vehicles, backup power sources for residential-use devices, main power sources for leisure-use, outdoor and other power-consuming devices in out-of-grid locations, and lighter weight, higher power density, ambient temperature-independent replacements for portable battery packs.

Because large scale, economic production of hydrogen, infrastructure required for its distribution, and practical means for its storage (especially as a transportation fuel) are widely believed to be a long way off, much current research and development has been directed to improving both fuel reformers as sources of electrochemically oxidizable fuels, notably mixtures of hydrogen and carbon monoxide, and fuel cell assemblies, commonly referred to as fuel cell “stacks,” as convertors of such fuels to electricity, and the integration of fuel reformers and fuel cells into more compact, reliable and efficient devices for the production of electrical energy.

SUMMARY OF THE INVENTION

In accordance with the present disclosure, there is provided a multi-tubular chemical reactor comprising a plurality of spaced-apart reactor units, each reactor unit comprising an elongate tube having a wall with internal and external surfaces, an inlet at one end and an outlet at the opposing end, the wall enclosing a gaseous flow passageway at least a portion of which defines a gas phase reaction zone, the multi-tubular chemical reactor can include at least one igniter for initiation of at least one gas phase exothermic reaction within a gas phase reaction zone of a reactor unit. The igniter can include a radiant heat-producing element positioned in thermal communication with and proximity to, but in physical isolation from, the gas phase reaction zone.

With respect to the plurality of spaced-apart reactor units, the maximum distance between adjacent reactor units can be during a steady-state mode of operation that distance beyond which the temperature of the plurality of spaced-apart reactor units falls below a predetermined minimum array temperature. The minimum distance between adjacent reactor units can be that distance below which the temperature at an outlet of a reactor unit is greater than a predetermined maximum temperature.

The multi-tubular chemical reactor can include at least one thermocouple disposed within a chamber comprising the plurality of spaced-apart reactor units.

The multi-tubular chemical reactor can include a plurality of igniters. At least one igniter can be disposed at one end of a chamber comprising the plurality of spaced-apart reactor units and at least one igniter being disposed at the opposite end of the chamber. The multi-tubular chemical reactor can include a plurality of igniters and a plurality of thermocouples disposed within a chamber comprising the plurality of spaced-apart reactor units. At least one igniter and at least one thermocouple can be disposed at one end of the chamber and at least one igniter and at least one thermocouple can be disposed at the opposite end of the chamber.

The plurality of igniters and the plurality of thermocouples can be disposed within the chamber such that at least one igniter at one end of the chamber can be opposite a thermocouple disposed at the opposite end of the chamber,

The multi-tubular chemical reactor can include a source of gaseous reactants, the source of gaseous reactants in fluid communication with the gas phase reaction zone(s) of the reactor unit(s).

The multi-tubular chemical reactor can include a controller for controlling the operation of the multi-tubular chemical reactor. The controller can be in operative communication with the at least one igniter, and if present, at least one of the at least one thermocouple and the source of gaseous reactants.

In accordance with the present disclosure, there is provided a multi-tubular chemical reactor comprising: a plurality of spaced-apart reactor units aligned in a single row or parallel rows of essentially identical configuration aligned along a common longitudinal axis corresponding to line of length X, line L extending from the first to the last reactor disposed within a row, each reactor unit in a row comprising an elongate tube having a wall with internal and external surfaces, an inlet at one end and an outlet at the opposing end, the wall enclosing a gaseous flow passageway at least a portion of which defines a gas phase reaction zone; and, at least one igniter for the initiation of at least one gas phase exothermic reaction within the gas phase reaction zones of the reactor units, the igniter including a radiant heat-producing element positioned in proximity to, but in physical isolation from, exposed sections of reactor units, the length of such heat-producing element extending from at least about 30 percent up to about 100 percent of length X of line L.

In accordance with the present disclosure, there is provided a multi-tubular chemical reactor comprising: a plurality of spaced-apart reactor units, each reactor unit comprising an elongate tube having a wall with internal and external surfaces, an inlet at one end and an outlet at the opposing end, the wall enclosing a gaseous flow passageway at least a portion of which defines a gas phase reaction zone; and at least one igniter for the initiation of a plurality of gas phase exothermic reactions within the gas phase reaction zones of the reactor units, the igniter including a radiant heat-producing element positioned in proximity to, but in physical isolation from, exposed sections of reactor units, the length of such heat-producing element extending such that it is in proximity to a plurality of the gas phase reaction zones of the reactor units.

The CPOX gas phase reaction zones of the CPOX reactor units and the heat-radiating element of each igniter can be disposed within a thermally insulated chamber. Operation of an igniter can transmit radiant heat via its heat radiating element to the CPOX gas phase reaction zone of at least one CPOX reactor unit in proximity thereto to initiate at least one gas phase exothermic reaction within such reaction zone.

The igniter component of the multi-tubular gas phase chemical reactor, physically isolated as it is from the reaction zones of CPOX reactor units disposed within the thermally insulated chamber, provides several benefits and advantages for the management of reactor operation. Depending on the number and arrangement of tubular reactor units in a row or parallel rows, a single igniter unit, and at most only a few igniter units, can often suffice to initiate, or light-off; one or more exothermic gas phase reactions within the gas phase reaction zones of the reactor units. This simplifies both the construction of the reactor and its individual tubular reactor units, the operation of the reactor and the identification and replacement of an inoperative or defective igniter should such be required.

Another major advantage of the igniter component of the reactor herein is the ease with which it can be deactivated once steady-state operation of the reactor is achieved and reactivated to once again initiate exothermic gas phase reaction as the management of the reactor operations require. The facility of activating and deactivating the igniter can be a benefit for multi-tubular reactors that in their normal functioning may undergo frequent and rapid on-off cycles.

In accordance with the present disclosure, there is provided a start-up method for a multi-tubular chemical reactor comprising the steps of: initiating maximum heating in all of the igniters; determining initiation of a gas phase exothermic reactions within centrally located reactor units; reducing heating of outer igniters to a first heating level reducing heating of inner igniters to a second heating level, the second heating level being less than the first heating level; determining initiation of a gas phase exothermic reactions within outer located reactor units; turning off the heating of the igniters.

BRIEF DESCRIPTION OF THE DRAWINGS

It should be understood that the drawings described below are for illustration purposes only. The drawings are not necessarily to scale, with emphasis generally being placed upon illustrating the principles of the present teachings. The drawings are not intended to limit the scope of the present teachings in any way. Like numerals generally refer to like parts.

FIG. 1 is a schematic block diagram of a known type of, gas phase exothermic chemical reactor, specifically, a gaseous fuel CPOX reformer featuring multiple tubular gas phase CPOX reactor units.

FIG. 2 is a schematic block diagram of an of an embodiment of gas phase exothermic chemical reactor, specifically, a gas phase CPOX reformer, in accordance with the present teachings.

FIG. 3 is schematic block diagram of an exemplary control system for managing the operation of the gaseous fuel CPOX reformer of FIGS. 1 and 2 .

FIG. 4 is a flowchart of an exemplary control routine executed by a controller for managing the operation of the gaseous fuel CPOX reformer routine executed by a controller such as the control system illustrated in FIG. 3 .

FIG. 5A is a longitudinal cross section view of an embodiment of an embodiment of gaseous fuel CPOX reformer constructed in accordance with the present teachings.

FIG. 5B is a lateral (perpendicular to the longitudinal axis) cross section view of the gaseous fuel CPOX reformer illustrated in FIG. 5A.

FIG. 5C is a plan cross section view of a portion of the gaseous fuel CPOX reformer illustrated in FIG. 5A.

FIG. 5D is an exploded perspective view of the embodiment of the gaseous fuel CPOX reactor of FIGS. 2 and 5A showing, inter alia, the disposition of rows of tubular gas phase CPOX reactor units and their gas phase CPOX reaction zones within thermally insulated chamber.

FIG. 6 is a longitudinal cross section view of another embodiment of gas phase chemical reactor, specifically, a liquid fuel CPOX reformer, in accordance with the present teachings.

FIG. 7 is a flowchart of an exemplary control routing executed by a controller for managing the operation of the liquid fuel CPOX reformer of FIG. 6 .

FIGS. 8A-8C are diagrams illustrating a start-up procedure of the gas phase chemical reactor in accordance with the present teachings.

DETAILED DESCRIPTION OF THE INVENTION

It is to be understood that although the present description is described as applying to a CPOX reformer, the present disclosure applies to all exothermic reformers and/or reactions.

It is also to be understood that the present teachings herein are not limited to the particular procedures, materials and modifications described and as such can vary. It is also to be understood that the terminology used is for purposes of describing particular embodiments only and is not intended to limit the scope of the present teachings which will be limited only by the appended claims.

For brevity, the discussion and description herein will mainly focus on catalyzed partial oxidation reforming reactions and reactants including catalytic partial oxidation reforming reactions and reactants (a reformable fuel and an oxygen-containing gas). However, the devices, assemblies, systems and methods described herein can apply to other exothermic reforming reactions such as autothermal reforming and reactants (a reformable fuel, steam and an oxygen-containing gas) as well as other gas phase exothermic reactions described herein. Accordingly, where an oxygen-containing gas is referenced herein in connection with a device or method, the present teachings should be considered as including steam in combination with an oxygen-containing gas unless explicitly stated otherwise or understood by the context. In addition, where a reformable fuel is referenced herein in connection with a device or method, the present teachings should be considered as including steam in combination or alone, i.e., a reformable fuel and/or steam, unless explicitly stated otherwise or as understood by the context.

In addition, the reactors, systems and methods of the present teachings should be understood to be suitable to carry out CPOX reforming and autothermal reforming, for example, occurring within the same structure and components and/or with the same general methods as described herein. That is, the reactors, systems and methods of the present teachings can deliver the appropriate liquid reactants, for example, liquid reformable fuel and/or liquid water, from a liquid reformable fuel reservoir to a vaporizer to create a vaporized liquid reformable fuel and steam, respectively, and the appropriate gaseous reactants, for example, at least one of an oxygen-containing gas, a gaseous reformable fuel and steam, from their respective sources to a desired component of a fuel cell unit or system for example, a reformer.

Where water is used in the delivery system, recycled heat from one or more of a reformer, a fuel cell stack and an afterburner of a fuel cell unit or system can be used to vaporize the water to create steam, which can be present in the delivery system and/or introduced into the delivery system from an independent source.

Throughout the specification and claims, where structures, devices, apparatus, compositions, etc., are described as having, including or comprising specific components, or where methods are described as having, including or comprising specific method steps, it is contemplated that such structures, devices, apparatus, compositions, etc., also consist essentially of, or consist of, the recited components and that such methods also consist essentially of, or consist of, the recited method steps.

In the specification and claims, where an element or component is said to be included in and/or selected from a list of recited elements or components, it should be understood that the element or component can be any one of the recited elements or components, or the element or component can be selected from a group consisting of two or more of the recited elements or components. Further, it should be understood that elements and/or features of a structure, device, apparatus or composition, or a method described herein, can be combined in a variety of ways without departing from the focus and scope of the present teachings whether explicit or implicit therein. For example, where reference is made to a particular structure, that structure can be used in various embodiments of the apparatus and/or method of the present teachings.

The use of the terms “include,” “includes,” “including,” “have,” “has,” “having,” “contain,” “contains,” or “containing,” including grammatical equivalents thereof, should be generally understood as open-ended and non-limiting, for example, not excluding additional unrecited elements or steps, unless otherwise specifically stated or understood from the context.

The use of the singular herein, for example, “a,” “an,” , and “the,” includes the plural (and vice versa) unless specifically stated otherwise.

Where the use of the term “about” is before a quantitative value, the present teachings also include the specific quantitative value itself, unless specifically stated otherwise. As used herein, the term “about” refers to a ±10% variation from the nominal value unless otherwise indicated or inferred.

It should be understood that the order of steps or order for performing certain actions is immaterial so long as the present teachings remain operable. For example, the methods described herein can be performed in any suitable order unless otherwise indicated herein or otherwise clearly contradicted by context. Moreover, unless steps by their nature must be conducted in sequence, they can be conducted simultaneously.

At various places in the present specification, numerical values are disclosed as ranges of values. It is specifically intended that a range of numerical values disclosed herein include each and every value within the range and any subrange thereof. For example, a numerical value within the range of from 0 to 20 is specifically intended to individually disclose 0, 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19 and 20 and any subrange thereof, for example, from 0 to 10, from 8 to 16, from 16 to 20, etc.

The use of any and all examples, or exemplary language provided herein, for example, “such as,” is intended merely to better illuminate the present teachings and does not pose a limitation on the scope of the invention unless claimed. No language in the specification should be construed as indicating any non-claimed element as essential to the practice of the present teachings.

Terms and expressions indicating spatial orientation or attitude such as “upper,” “lower,” “top,” “bottom,” “horizontal,” “vertical,” and the like, unless their contextual usage indicates otherwise, are to be understood herein as having no structural, functional or operational significance and as merely reflecting the arbitrarily chosen orientation of the various views of reactors of the present teachings illustrated in certain of the accompanying figures.

As used herein, a “reformable fuel” refers to a liquid reformable fuel and/or a gaseous reformable fuel.

The expression “gaseous reformable fuel” shall be understood to include reformable carbon- and hydrogen-containing fuels that are a gas at STP conditions, for example, methane, ethane, propane, butane, isobutane, ethylene, propylene, butylene, isobutylene, dimethyl ether, their mixtures, such as natural gas and liquefied natural gas (LNG), which are mainly methane, and petroleum gas and liquefied petroleum gas (LPG), which are mainly propane or butane but include all mixtures made up primarily of propane and butane, and ammonia, and the like, that when subjected to reforming undergo conversion to hydrogen-rich reformates.

The expression “liquid reformable fuel” shall be understood to include reformable carbon- and hydrogen-containing fuels that are a liquid at standard temperature and pressure (STP) conditions, for example, methanol, ethanol, naphtha, distillate, gasoline, kerosene, jet fuel, diesel, biodiesel, and the like, that when subjected to reforming undergo conversion to hydrogen-rich reformates. The expression “liquid reformable fuel” shall be further understood to include such fuels whether they are in the liquid state or in the gaseous state, i.e., a vapor.

As used herein, “gaseous reforming reaction mixture” refers to a mixture including a gaseous liquid reformable fuel (e.g., a vaporized liquid reformable fuel), a gaseous reformable fuel or combinations thereof, and an oxygen-containing gas (e.g., air) and/or water (e.g., in the form of steam) in the case of autothermal reforming. A gaseous reforming reaction mixture can be subjected to a reforming reaction to create a hydrogen-rich product (“reformate”), which also can contain carbon monoxide. Where a catalytic partial oxidation reforming reaction is to be carried out, the gaseous reforming reaction mixture can be referred to a “gaseous CPOX reforming reaction mixture,” which includes a reformable fuel and an oxygen-containing gas. Where an autothermal reforming reaction is to be carried out, the gaseous reforming reaction mixture can be referred to as a “gaseous AT reforming reaction mixture,” which includes a reformable fuel, an oxygen-containing gas and steam.

The term “reforming reaction” shall be understood to include the exothermic reaction(s) that occur during the conversion of a gaseous reaction medium to a hydrogen-rich reformate. The expression “reforming reaction” herein therefore includes, for example, CPOX and autothermal reforming.

Again, as stated previously for brevity, the discussion and description herein will focus on partial oxidation reforming reactions and reactants including catalytic partial oxidation reforming reactions and reactants (a reformable fuel and an oxygen-containing gas). However, the devices, assemblies, systems and methods described herein can equally apply to other reforming reactions such as autothermal reforming and their respective reactants. For example, for autothermal reforming, steam can be introduced along with an oxygen-containing gas and/or a reformable fuel in the description herein.

The gas phase reactor of the disclosure will now be specifically described in detail by way of contrast to the known type of gaseous fuel CPOX reformer schematically illustrated in FIG. 1 .

FIGS. 2 and 5A-5D illustrate embodiments of gaseous fuel CPOX reactors constructed in accordance with the principles of the present invention, and FIG. 6 illustrates an exemplary liquid fuel CPOX reformer.

As shown in FIG. 1 , gaseous fuel CPOX reformer 1100 includes centrifugal blower 1102 for introducing oxygen-containing gas, exemplified here and in the other embodiments of the present teachings by air, into conduit 1103, and for driving this and other gaseous streams (inclusive of gaseous fuel-air mixture(s) and hydrogen-rich reformates) through the various passageways of the CPOX reformer. Conduit 1103 can include flow meter 1104 and thermocouple 1105. These and similar devices can be placed at various locations within a gaseous fuel CPOX reformer in order to measure, monitor and control the operation of the gaseous fuel CPOX reformer as more fully explained in connection with the control system illustrated in FIG. 3 .

In a start-up mode of operation of exemplary gaseous fuel CPOX reformer 1100, air introduced by blower 1102 into conduit 1103 combines with gaseous reformable fuel, exemplified here and in the other embodiments of the present teachings by propane, introduced into conduit 1103 at a relatively low pressure from gaseous fuel storage tank 1113 through fuel line 1114 equipped with optional thermocouple 1115, flow meter 1116 and flow control valve 1117. The air and propane combine in mixing zone 1118 of conduit 1103. A mixer, for example, a static mixer such as in-line mixer 1119, and/or vortex-creating helical grooves formed within the internal surface of conduit 1103, or an externally powered mixer (not shown), can be disposed within mixing zone 1118 of conduit 1103 to provide a more uniform propane-air gaseous CPOX reaction mixture than would otherwise be the case.

The propane-air mixture (i.e., gaseous CPOX reaction mixture) enters manifold, or plenum, 1120 which distributes the reaction mixture to the inlets of tubular CPOX reactor units 1109 and 1110. In a start-up mode of operation of CPOX reformer 1100, igniter 1123 a presenting heat-radiating element 1123 b, described in greater detail in connection with gaseous fuel CPOX reformer of FIGS. 1 and 5A-5D, initiates the exothermic gaseous phase CPOX reaction of the gaseous CPOX reaction mixture within gas phase CPOX reaction zones 1110 of tubular CPOX reactor units 1109 thereby commencing the production of hydrogen-rich reformate. Once steady-state CPOX reaction temperatures have been achieved (e.g., 150° C. to 1,100° C.), the exothermic reaction becomes self-sustaining and operation of the igniter(s) can be discontinued. Thermocouple 1125 is positioned proximate to one or more CPOX reaction zones 1110 to monitor the temperature of the CPOX reaction occurring within CPOX reactor units 1109, the temperature measurement being relayed as a monitored parameter to reformer control system 1126.

As shown in FIG. 1 , reformer 1100 includes multiple tubular CPOX reactor tubes 1100 aligned in at least one row, and, typically, at least one parallel pair of rows (e.g., as shown in the embodiments of CPOX reactor of this invention illustrated in FIGS. 5B, 5C and 5D) arranged along a common longitudinal axis defined by line L having a length X as measured from the center of the first reactor tube in a row to the center of the last reactor in the row. The gas phase CPOX reaction zones of tubular CPOX reactor units 1109 and 1110 are advantageously disposed within thermally insulated chamber 1128 so that heat of CPOX exotherm produced during steady state operation of reformer 1100 may be more readily recovered and utilized if desired, e.g., for the preheating of air, gaseous fuel and/or other gaseous stream(s) within the reformer, or vaporizing a liquid fuel. In the embodiment of known type reformer 1100 of FIG. 1 , it will be noted that heat radiating element, e.g., 1123 b of igniter 1123 a thereof, projects within thermally insulated chamber 1128 at one end thereof and terminates just a short distance beyond second CPOX reactor unit 1110, a distance that corresponds to approximately 20-25 percent of distance X of line L.

Reformer 1100 can also include a source of electrical current, for example, rechargeable lithium-ion battery system 1127, to provide power for its electrically driven components such as blower 1102, flow meters 1104 and 1116, flow control valve 1117 and igniter 1123 a.

If desired, product effluent, for example, hydrogen-rich reformate, from a gaseous fuel CPOX reformer can be introduced into one or more conventional or otherwise known carbon monoxide removal devices for the reduction of its carbon monoxide (CO) content, for example, where the product effluent is to be introduced as fuel to a fuel cell stack utilizing a catalyst that is particularly susceptible to poisoning by CO, such as is common to a polymer electrolyte membrane fuel cell. Thus, for example, the product effluent can be introduced into a water gas shift (WGS) converter wherein CO is converted to carbon dioxide (CO₂) while at the same time producing additional hydrogen, or the product reformate effluent can be introduced into a reactor wherein CO is made to undergo preferential oxidation (PROX) to CO₂. CO reduction can also be carried out employing a combination of these processes, for example, WGS followed by PROX and vice versa. It is also within the scope of the present teachings to reduce the level of CO in the product reformate by passage of the product reformate through a known or conventional clean-up unit or device equipped with a hydrogen-selective membrane providing separation of the product reformate into a hydrogen stream and a CO containing by-product stream. Units/devices of this kind can also be combined with one or more other CO-reduction units such as the aforementioned WGS converter and/or PROX reactor.

Gas phase CPOX reactor 100 of FIG. 2 , constructed in accordance with the principles of the invention, is identical to gas phase CPOX reactor 1100 of FIG. 1 except with respect to the percentages of length X of line L that heat-radiating element 1123 b of igniter 1123 of CPOX reactor 1100 and corresponding heat-radiating element 123 b of igniter 123 of CPOX reactor 100 extend along the length of line I. In all other respects, reactors 1100 of FIG. 1 and 100 of FIG. 2 are identical therefore dispensing with the need for a separate and repetitive description of CPOX reactor 100 except for aforenoted difference in structure between the two reactors having to do with the length of heat radiating elements 1123 b and 123 b, respectively in relation to line L. As previously noted, in the case of heat-radiating element 1123 b of CPOX reactor 1100, the length X to which such element 1123 b extends along line L does not exceed about 25 percent of such length. In contrast to the foregoing maximum length of heat-radiating element 1123 b of CPOX reactor 1100 of FIG. 1 . (PRIOR ART), heat-radiating element 123 b of CPOX reactor 100 of FIG. 2 extends a distance X which is at least about thirty percent, preferably at least about sixty percent, and more preferably still, about one hundred percent of the length of line L and if desired, an even greater distance, e.g., from about 5 to about 10 percent, beyond the length of line L as shown in the embodiments of CPOX reactors of FIGS. 2 and 5 . The significantly greater distance by which heat -producing element 123 b extends along line L in the case of CPOX reactor 100 of FIG. 2 has the very desirable effect of reducing the time for initiating self-sustaining CPOX within the reaction zones of its CPOX reactor tubes , e.g., by at least about 10 to about 20 percent, preferably by at least about 20 to at least about 40 and more preferably, by at least about 40 to at least about 60 less time than it takes to initiate self-sustaining CPOX in such reactor and, surprisingly, without the need to deliver a significantly greater degree of electrical power (in the case where heat radiating element 123 b is an electrical resistance element).

The power provided by 1123B was 20 W and the power provided by 123B was 40W. More importantly, the Watts/unit length is reduced from the shorter, lower power unit, which had a significantly higher heat density. This configuration tended to run the risk of overheating the immediately local catalyst and causing auto-ignition or vaporizing catalyst (>1000 C) prior to full thermal communication and bed ignition. The longer heater provides a more uniform and controlled heat source for a preferential startup condition

While it may be possible to reduce the time required for initiation of self-sustaining CPOX by employing mutually opposed igniters disposed at opposite ends of thermally insulated chamber 1128 (as in the embodiments of the CPOX reactors shown in FIGS. 5C and 5D), it will be readily recognized and appreciated that the solution herein to the goal of achieving significantly reduced, that is to say, faster, CPOX initiation times as exemplified by the embodiment of single igniter CPOX reactor 100 shown in FIG. 3 is a simpler design (and one that is therefore simpler to manufacture) for achieving the same goal.

Exemplary control system 200 illustrated in FIG. 3 is provided for controlling the operations of a gaseous fuel CPOX reformer in accordance with the present teachings, e.g., CPOX reformer 100 of FIG. 2 and reformer 400 of FIGS. 5A-5D. As those skilled in the art will readily recognize, with suitable modification to take into account the operations of the air-preheating and liquid fuel-vaporizing components of liquid fuel CPOX reformer 500 of FIG. 6 , control system 200 can also be used for controlling the operations of this type of reformer as well.

As shown in FIG. 2 , control system 200 includes controller 201 to manage gaseous fuel CPOX reformer 202 in its start-up, steady-state, and shut-down modes of operation. The controller can be software operating on a processor. However, it is within the scope of the present teachings to employ a controller that is implemented with one or more digital or analog circuits, or combinations thereof.

Control system 200 further includes a plurality of sensor assemblies, for example, thermocouple and associated fuel pressure meter 204, thermocouple and associated air pressure meter 209, and reformer thermocouple 214, in communication with controller 201 and adapted to monitor selected operating parameters of CPOX reformer 202.

In response to input signals from the sensor assemblies, user commands from a user-input device and/or programmed subroutines and command sequences, controller 201 can manage the operations of a gaseous fuel CPOX reformer in accordance with the present teachings. More specifically, controller 201 can communicate with a control signal-receiving portion of the desired section or component of a gaseous fuel CPOX reformer by sending command signals thereto directing a particular action. Thus, for example, in response to flow rate input signals from thermocouple and associated pressure meters 204 and 209 and/or temperature input signals from reformer thermocouple 214, controller 201 can send control signals to fuel flow control valve 205, for example, to control the flow of fuel from gaseous fuel storage tank 203 through fuel line 206 to conduit 207, to centrifugal blower 208 to control the flow of air into conduit 207 and drive the flow of gaseous CPOX reaction mixture within and through CPOX reformer 202, to igniter 211 to control its on-off states, and to battery/battery recharger system 212 to manage its functions.

The sensor assemblies, control signal-receiving devices and communication pathways herein can be of any suitable construction and of those known in the art. The sensor assemblies can include any suitable sensor devices for the operating parameters being monitored. For example, fuel flow rates can be monitored with any suitable flow meter, pressures can be monitored with any suitable pressure-sensing or pressure-regulating device, and the like. The sensor assemblies can also, but do not necessarily, include a transducer in communication with the controller. The communication pathways will ordinarily be wired electrical signals but any other suitable form of communication pathway can also be employed.

In FIG. 2 , communication pathways are schematically illustrated as single- or double-headed arrows. An arrow terminating at controller 201 schematically represents an input signal such as the value of a measured flow rate or measured temperature. An arrow extending from controller 201 schematically represents a control signal sent to direct a responsive action from the component at which the arrow terminates. Dual-headed pathways schematically represent that controller 201 not only sends command signals to corresponding components of CPOX reformer 202 to provide a determined responsive action, but also receives operating inputs from CPOX reformer 202 and mechanical units such as fuel control valve 205 and blower 208 and measurement inputs from sensor assemblies such as pressure meters 204 and 209 and thermocouple 214.

FIG. 4 presents a flow chart of an exemplary control routine that can be executed by a controller of a control system to automate the operations of a gaseous fuel CPOX reformer, e.g., reformer 100 of FIG. 2 and reformer 400 of FIGS. 5A-5 .D. The flow chart can be executed by a controller at a fixed interval, for example, every 10 milliseconds or so. The control logic illustrated in FIG. 4 performs several functions including the management of gaseous flows and CPOX reaction temperatures in start-up and steady-state modes of operation and management of the procedure for the shut-down mode of reformer operation.

As shown in the various views of exemplary gaseous fuel CPOX reformer 400 and components thereof illustrated in FIGS. 5A-5D, which are representative of further embodiments of the present teachings, air as an oxygen-containing gas, typically at ambient temperature, is introduced at a preset mass flow rate via centrifugal blower 402 through inlet 403 of conduit 404. Propane is introduced into conduit 404 via fuel line 441 and fuel inlet 442. Propane and air begin to combine in mixing zone 420 of conduit 404 to provide a gaseous CPOX reaction mixture. A mixer of any suitable kind, for example, a static mixer disposed within mixing zone 420 and/or a helically-grooved internal wall surface of conduit 404, can be included to provide a gaseous CPOX reaction mixture of greater compositional uniformity than otherwise would form in mixing zone 420.

Following its passage through the optional static mixer and/or contact with helical grooves disposed within mixing zone 420, gaseous CPOX reaction mixture exits conduit 404 through outlet 425 and into fuel distribution manifold 426. From manifold 426, gaseous CPOX reaction mixture enters inlets 431 of CPOX reactor units 408 and into CPOX reaction zones 409 where the reaction mixture undergoes exothermic gas phase CPOX reaction to produce a hydrogen-rich, carbon monoxide-containing reformate. In the start-up mode, one or more igniters 435 initiates CPOX. After CPOX becomes self-sustaining, for example, when the temperature of the reaction zone reaches from about 250° C. to about 1100° C., igniter(s) 435 can be shut off as external ignition is no longer required to maintain the now self-sustaining exothermic CPOX reaction. Thermal insulation 410, for example, of the microporous or alumina-based refractory type, surrounds those portions of CPOX reformer 400 to reduce thermal losses from these components.

FIGS. 5A-5D illustrate an embodiment of the present teachings where two igniters 435 (one for each separate array of CPOX reactor units 408) are utilized to initiate CPOX reaction within exothermic CPOX reaction zones 409 of CPOX reactor units 408 disposed within and/or extending through chamber 436 during the start-up mode of operation of reformer 400. As shown in FIGS. 5C and 5D, CPOX reactor units 408 are arranged in two separate pairs of parallel rows of tubular CPOX reactor units(specifically,7 reactor units in the embodiment shown although rows containing more or less than this number of CPOX reactor units and/or arranged other than in parallel, e.g., in a sawtooth pattern are contemplated) disposed within thermally insulated chamber 436, with one pair of rows flanking one side of conduit 404 and the other such pair of rows flanking the other side of conduit 404. The perimeter of a pair of rows of CPOX reactor tubes marks the boundary between open space 438 of thermally insulated chamber 436 and thermal insulation 410. Exterior surfaces 437 of the walls of CPOX reactor units 408 corresponding to at least a portion of their CPOX reaction zones 409 are exposed within open space 438. Igniters 435 of the electrical resistance type, for example, rated at from 10 to 80 watts or greater, are disposed at opposing ends of thermally insulated chamber 436 where their radiant heat-producing elements 439 are positioned in proximity to, but in physical isolation from, exterior surfaces 437 of CPOX reactor units 408. Thermocouples 440 are disposed at the ends of chamber 436 opposing igniters 435 in order to monitor the temperature of CPOX reaction zones 409 and provide a reformer control input as described in connection with control system 200 illustrated in FIG. 3 . Operation of the igniters causes radiant heat to be transferred to, and through, the walls of one or more nearby CPOX reactor units whereby CPOX is initiated within the CPOX reaction zone of such reactor unit(s). The thermal radiation emitted from the CPOX reaction zone(s) of these nearby CPOX reactor units can then initiate CPOX within the reaction zones of the remaining CPOX reactor units within the rows of CPOX reactor units as illustrated by the wavy arrows in FIG. 5C.

The provision of a single, or at most a few, igniter(s) 435 that avoid direct contact with the gas phase reaction zones of CPOX reactor units 408 provides several advantages over a CPOX igniter system in which each CPOX reactor unit has its own physically attached or integrated igniter. Identification of an inoperative igniter can be problematic and its removal and replacement without damage to the CPOX reactor unit of which it is a part and/or disturbance to other reactor units in a row of CPOX reactor units can be difficult. Accordingly, a single or just a few igniters with their heat-radiating elements suitably positioned close to a row or pair of rows of CPOX reactor units but avoiding physical contact with a reactor unit therein, e.g., an igniter's heat-radiating element disposed equidistantly between two rows of CPOX reactor units as shown in the embodiments of CPOX reformers illustrated in FIGS. 5B, 5C and 5D) can permit easy and simple identification and extraction from CPOX reformer 400 of a failed or defective igniter, and its replacement with an operative igniter.

As shown in FIGS. 5C and 5D where two igniters are used to initiate the CPOX reaction within CPOX reaction zones 409 of CPOX reactor units 408, it can be advantageous to reverse the positions of igniter 435 and thermocouple 440 on one side of chamber 436 relative to the positions of igniter 435 and thermocouple 440 on the other side of the thermally insulated chamber, particularly where there can be significant thermal communication between the two chambers. Such an arrangement has been observed to result in a more rapid initiation of CPOX within the CPOX reaction zones of each separate array of CPOX reactor units. However, it should be understood that with appropriately dimensioned and positioned CPOX reactor units within a chamber, a single igniter can be used to initiate CPOX within the CPOX reaction zones of the CPOX reactor units within the chamber.

As those skilled in the art will readily recognize and appreciate, the cross sectional configuration, number and dimensions of CPOX reactor units and the distances of their separation from each other measured from their geometric centers, or centroids, will be made to depend on the operational and mechanical performance specifications for a particular gaseous fuel CPOX reactor. In the case of a CPOX reactor unit of substantially uniform circular cross section, for example, CPOX reactor unit 408 illustrated in FIGS. 4C and 4D, the number of such CPOX reactor units, their length and their internal and external diameters (defining the thickness of their gas-permeable walls) the gas-permeable walls will be determined by, among other things, the hydrogen-producing capacity of the CPOX reformer, which in turn is a function of several factors including the type, amount (loading and distribution of CPOX catalyst within the gas-permeable walls), the characteristics of the porous structure of walls (characteristics influencing the gas-permeability of the walls and therefore affecting the CPOX reaction) such as pore volume (a function of pore size), the principal type of pore (mostly open, i.e., reticulated, or mostly closed, i.e., non-reticulated), and pore shape (spherical or irregular), the volumetric flow rates of CPOX reaction mixture, CPOX temperature, back pressure, and the like.

The desired mechanical performance characteristics of a particular gaseous fuel CPOX reformer will depend to a considerable extent on such factors as the thermal and mechanical properties of the material used for construction of the CPOX reactor units, the volume and morphology of the pores of the gas-permeable structure of the walls of the CPOX reactor units, the dimensions of the reactor units, particularly wall thickness, and related factors.

For a gaseous fuel CPOX reformer to suitably function, the gas permeability property of the catalytically active wall structure of a tubular CPOX reactor unit enclosing a gaseous phase CPOX reaction zone should be such as to allow gaseous reformable fuel to enter freely and diffuse through such wall structure thereby making effective contact not only with surface CPOX catalyst but interior CPOX catalyst as well, if present. It should be noted that CPOX reactor unit wall structures having limited gas permeability for the vaporized reformable fuel can be mass transport limited so as to impede significantly CPOX conversion of the gaseous reformable fuel to hydrogen-rich reformate. By contrast, catalytically active reactor wall structures of suitable gas permeability promote CPOX conversion of the gaseous reformable fuel and selectivity for hydrogen-rich reformates of desirable composition.

Guided by the present teachings and employing known and conventional testing procedures, those skilled in the art can readily construct CPOX reactor units having catalytically active wall structures exhibiting optimal gas permeability properties for a particular gaseous reformable fuel to be processed.

Materials from which the catalytically active wall structure of a CPOX reaction zone of a tubular CPOX reactor unit can be fabricated are those that enable such wall structures to remain stable under the high temperatures and oxidative environments characteristic of CPOX reactions. Conventional and otherwise known refractory metals, refractory ceramics, and combinations thereof can be used for the construction of the catalytically active wall structure of a CPOX reaction zone. Some of these materials, for example, perovskites, can also possess catalytic activity for partial oxidation and therefore can be useful not only for the fabrication of the catalytically active wall structure of a CPOX reaction zone but can also supply part or even all of the CPOX catalyst for such structure.

Among the useful refractory metals are titanium, vanadium, chromium, zirconium, molybdenum, rhodium, tungsten, nickel, iron and the like, their combinations with each other and/or with other metals and/or metal alloys, and the like. Refractory ceramics are an especially attractive class of materials for the construction of the catalytically active wall structures due to their relatively low cost compared to many of the refractory metals and metal alloys that are also useful for this purpose. The comparative ease with which such ceramics can be formed into tubular gas-permeable structures of fairly reproducible pore type employing known and conventional pore-forming procedures and the generally highly satisfactory structural/mechanical properties of ceramics (including coefficients of thermal expansion and thermal shock performance) and resistance to chemical degradation make them particularly advantageous materials. Suitable refractory ceramics for the construction of a CPOX reaction zone (which as previously stated, can include the entire wall structure of a CPOX reactor unit) include, for example, perovskites, spinels, magnesia, ceria, stabilized ceria, silica, titania, zirconia, stabilized zirconia such as alumina-stabilized zirconia, calcia-stabilized zirconia, ceria-stabilized zirconia, magnesia-stabilized zirconia, lanthana-stabilized zirconia and yttria-stabilized zirconia, zirconia stabilized alumina, pyrochlores, brownmillerites, zirconium phosphate, silicon carbide, yttrium aluminum garnet, alumina, alpha-alumina, gamma-alumina, beta-alumina, aluminum silicate, cordierite, MgAl₂O₄, and the like, various ones of which are disclosed in U.S. Pat. Nos. 6,402,989 and 7,070,752, the entire contents of which are incorporated by reference herein; and, rare earth aluminates and rare earth gallates various ones of which are disclosed in U.S. Pat. Nos. 7,001,867 and 7,888,278, the entire contents of which are incorporated by reference herein.

In general, the total or overall fuel conversion capacity of a CPOX reformer of a given design will be the sum of the fuel conversion capabilities of its individual CPOX reactor units. The minimum distance between adjacent CPOX reactor units will be such that in the steady-state mode of operation of the reformer, the temperature of the reactor units does not exceed a predetermined, or preset, maximum, and the maximum distance between adjacent CPOX reactor units is that distance beyond which the temperature within one or more CPOX reactor units falls below a predetermined, or preset, minimum intended for the steady-state mode of operation of the reformer. Within the above principles as guidance, the minimum and maximum distances between adjacent CPOX reactor units can be determined for a given reformer design employing routine testing methods.

More specifically, the maximum distance can be that distance beyond which, during a steady-state mode of operation, the temperature of the array of spaced-apart CPOX reactor units falls below a predetermined minimum array temperature. Depending on various factors, including those discussed herein, the predetermined minimum array temperature of an array of spaced-apart CPOX reactor units during steady-state mode of operation can be about 550° C., about 575° C., about 600° C., about 625° C., about 650° C., about 675° C., about 700° C., about 725° C., about 750° C., about 775° C., about 800° C., about 825 ° C., or about 850 C.

The minimum distance between adjacent CPOX reactor units can be that distance below which the temperature at an outlet of a CPOX reactor unit is greater than a predetermined maximum temperature. The predetermined maximum temperature can be a temperature that is tolerable by an inlet of a fuel cell stack in thermal and fluid communication with an outlet of a CPOX reactor unit, for example, a temperature at which the seals of the inlets of the fuel cell stack do not degrade and remain functional. Depending on various factors, including those discussed herein, the predetermined maximum temperature of a CPOX reactor unit can be about 775° C., about 800° C., about 825° C., about 850° C., about 875° C., about 900° C., about 925° C., about 950° C., about 975° C., or about 1000° C.

The present teachings contemplate the use of any of the heretofore known and conventional CPOX catalysts (including catalyst systems), methods of incorporating catalyst within a porous substrate or support, specifically, the gas-permeable wall of the CPOX reactor unit, and patterns of catalyst distribution including, but not limited to, catalyst confined to a particular section of a wall, catalyst loading increased along the length of a reactor unit and/or decreased from an inner surface of a wall to its outer surface, CPOX catalyst that varies in composition along the length of the reactor unit, and similar variants. Thus, for example, increasing catalyst loading within a wall of a CPOX reactor unit from the start of a CPOX reaction zone to, or near, the end thereof can be helpful in maintaining a constant CPOX reaction temperature within this zone.

Among the many known and conventional CPOX catalysts that can be utilized herein are the metals, metal alloys, metal oxides, mixed metal oxides, perovskites, pyrochlores, their mixtures and combinations, including various ones of which are disclosed, for example, in U.S. Pat. Nos. 5,149,156; 5,447,705; 6,379,586; 6,402,989; 6,458,334; 6,488,907; 6,702,960; 6,726,853; 6,878,667; 7,070,752; 7,090,826; 7,328,691; 7,585,810; 7,888,278; 8,062,800; and, 8,241,600, the entire contents of which are incorporated by reference herein.

While numerous highly active noble metal-containing CPOX catalysts are known and as such can be useful herein, they are generally less often employed than other known types of CPOX catalysts due to their high cost, their tendency to sinter at high temperatures and consequently undergo a reduction in catalytic activity, and their proneness to poisoning by sulfur.

Perovskite catalysts are a class of CPOX catalyst useful in the present teachings as they are also suitable for the construction of the catalytically active wall structures of a CPOX reactor unit. Perovskite catalysts are characterized by the structure ABX3 where “A” and “B” are cations of very different sizes and “X” is an anion, generally oxygen, that bonds to both cations. Examples of suitable perovskite CPOX catalysts include LaNiO₃, LaCoO₃, LaCrO₃, LaFeO₃ and LaMnO₃.

A-site modification of the perovskites generally affects their thermal stability while B-site modification generally affects their catalytic activity. Perovskites can be tailor-modified for particular CPOX reaction conditions by doping at their A and/or B sites. Doping results in the atomic level dispersion of the active dopant within the perovskite lattice thereby inhibiting degradations in their catalytic performance. Perovskites can also exhibit excellent tolerance to sulfur at high temperatures characteristic of CPOX reforming. Examples of doped perovskites useful as CPOX catalysts include La_(1-x)Ce_(x)FeO₃, LaCr_(1-y)Ru_(y)O₃, La_(1-x)Sr_(x)Al_(1-y)Ru_(y)O₃ and La_(1-x)Sr_(x)FeO₃ wherein x and y are numbers ranging, for example, from 0.01 to 0.5, for example, from 0.05 to 0.2, etc., depending on the solubility limit and cost of the dopants.

Liquid fuel CPOX reformer 500 illustrated in FIG. 5 and the exemplary control routine illustrated in FIG. 6 for the automated operation of reformer 500 are of a kind disclosed in benefit U.S. patent application Ser. No. 61/900,510.

As shown in exemplary liquid fuel CPOX reformer 500 of FIG. 6 which is further representative of the present teachings, air as an oxygen-containing gas is introduced at ambient temperature and at a preset mass flow rate via centrifugal blower 502 through inlet 503 of conduit 504, which includes a generally U-shaped conduit section favoring compact design. The ambient temperature air is initially heated in the start-up mode operation of the reformer to within a preset range of elevated temperature by passage through first heating zone 505 supplied with heat from electric heater 506 which can be of a conventional or otherwise known electrical resistance type rated, for example, at from 10 to 80 watts or even greater depending upon designed range of fuel processing capacity of reformer 500. Electrical resistance heaters are capable of raising the temperature of ambient air introduced into a conduit to a desired level for a relatively wide range of CPOX reformer configurations and operating capacities. During the steady-state mode of operation of reformer 500, electric heater 506 can be shut off, the air introduced into conduit 504 then being initially heated within second heating zone 507 by heat of exotherm recovered from CPOX reaction zones 509 of elongate tubular gas-permeable CPOX reactor units 508, for example, of the structure and composition described above in connection with CPOX reactor units 408 of gaseous fuel CPOX reformer 400 of FIG. 5A-5D. In this manner, the temperature of the air introduced into conduit 504 can be increased from ambient to within some preset elevated range of temperature with the particular temperature being influenced by a variety of design, i.e., structural and operational, factors as those skilled in the art will readily recognize.

As in the case of gaseous fuel CPOX reformer 400 of FIGS. 5A-5D, thermal insulation 510 advantageously surrounds heat-radiating portions of liquid fuel CPOX reformer 500 in order to reduce thermal losses therefrom.

To raise the temperature of the air that had been initially heated by passage through first heating zone 505 in a startup mode or through second heat zone 507 in a steady-state mode, as the initially heated air continues to flow downstream in conduit 504, it advantageously flows through optional third heating zone 512 supplied with heat from optional second electric heater unit 513. Because optional second electric heater unit 513 need only increase the temperature of the initially heated air by a relatively small extent, it can function as an incremental heater capable of making the typically small adjustments in air temperature that are conducive to precise and rapid thermal management of the reformer both with regard to the functioning of its fuel vaporization system and its tubular CPOX reactor units.

A liquid reformable fuel such as any of those mentioned above, and exemplified in this and the other embodiments of the present teachings by automotive diesel, is introduced via fuel line 514 terminating within conduit 504 in liquid fuel spreader device 515, for example, a wick (as shown) or spray device.

Any conventional or otherwise known pump or equivalent device 518 for passing fluid through the passageways and conduits of a liquid fuel CPOX reformer, for example, for introducing liquid fuel through fuel line 514 into conduit 504, can be used. For example, a metering pump, rotary pump, impeller pump, diaphragm pump, peristaltic pump, positive displacement pump such as a gerotor, gear pump, piezoelectric pump, electrokinetic pump, electroosmotic pump, capillary pump, and the like, can be utilized for this purpose. In some embodiments, pump or equivalent device 518 can deliver the fuel on an intermittent or pulsed flow basis. In certain embodiments, a pump or equivalent device can deliver the fuel as a substantially continuous flow. In particular embodiments, a pump or equivalent device can make rapid adjustments in fuel flow rate in response to changing CPOX reformer operating requirements.

As indicated above, the pressurized liquid fuel can be spread within a conduit by a wick or as a fine spray or otherwise in droplet form by any of such conventional or otherwise known spray devices as fuel injectors, pressurized nozzles, atomizers (including those of the ultrasonic type), nebulizers, and the like.

Heat produced by electric heater 506 within first heating zone 505 in a start-up mode or heat of exotherm recovered from CPOX within second heating zone 507 during a steady-state mode, combined, if desired, with heat produced by optional second electric heater 513 within optional heating zone 512 function in unison to vaporize the liquid fuel introduced into conduit 504 and together constitute the principal components of the fuel vaporizer system of the reformer.

Optional second electric heater 513 operates to not only incrementally raise the temperature of the initially heated ambient temperature air passing within its associated optional. third heating zone but can also be used to heat the liquid fuel prior to its introduction into conduit 504 thereby facilitating the vaporization of the fuel once it enters the conduit.

To provide for the heating of the liquid fuel before it enters main conduit 504, fuel line 514 traverses the wall of conduit 504 with section 519 of the fuel line being extended in length to prolong the residence time of fuel flowing therein where the fuel line passes through, or is proximate to, optional third heating zone 512 of main conduit 504. An extended fuel line section can assume a variety of configurations for this purpose, for example, a coiled or helical winding (as shown) or a series of lengthwise folds, disposed on or proximate to the exterior surface of a conduit corresponding to a second heating zone or any similar such configuration disposed within the interior of the conduit at or near the second heating zone. Regardless of its exact configuration and/or disposition, extended fuel line section 519 must be in effective heat transfer proximity to optional third heating zone 512 so as to receive an amount of heat sufficient to raise the temperature of the fuel therein to within some preset range of temperature. Thus, a portion of the thermal output of optional second electric heater 513 within third heating zone 512 of conduit 504, in addition to further heating air flowing within this zone, will transfer to fuel, for example, diesel fuel, flowing within the distal section 519 of fuel line 514, which distal section of fuel line 514 can be lengthened or extended as shown by reference numeral 519, thereby raising its temperature to within the preset range. Whichever range of temperature values is chosen for the fuel within the fuel line, it should not exceed the boiling point of the fuel (from 150° C. to 350° C. in the case of diesel) if vapor lock and consequent shut-down of reformer 500 are to be avoided.

Liquid fuel spreader 515 is disposed within conduit 504 downstream from optional second heating zone 512 and associated optional second electric heater 513 and upstream from mixing zone 520. Thermocouple 522 disposed within chamber 536 and thermocouple 523 is disposed within mixing zone 520 monitor, respectively, the temperatures of CPOX reforming occurring within CPOX reaction zones 509 of CPOX reactor units 508 and the temperature of the vaporized fuel-air mixture.

In the liquid fuel vaporizer systems described herein, there is no or at most little opportunity for the diesel to come into direct contact with a heated surface, for example, that of an electrical resistance heater element, that would pose a risk of raising the temperature of the diesel fuel to or above its flash point, to cause spattering of the fuel rather than its vaporization and/or cause pyrolysis of the fuel resulting in coke formation. Thus, the temperature of the diesel fuel can be readily and reliably maintained at a level below its flash point and without significant incidents of spattering or coking.

Following its passage through static mixer 521 disposed within mixing zone 520, gaseous CPOX reaction mixture exits main conduit 504 through outlet 525 and enters manifold 526. From manifold 526, the gaseous CPOX reaction mixture enters tubular CPOX reactor units 508 through inlets 531. The gaseous CPOX reaction mixture then enters CPOX reaction zones 509 where the mixture undergoes gaseous phase CPOX reaction(s) to produce a hydrogen-rich, carbon monoxide-containing reformate. In the start-up mode, at least one igniter 535, the heat-radiating element of which is disposed within chamber 536, is activated thereupon initiating CPOX. Igniter 535 and its operation are essentially identical to igniter 435 of gaseous fuel CPOX reformer 400 and the latter's operation. After CPOX becomes self-sustaining, for example, when the temperature of reaction zone 509 reaches from about 250° C. to about 1100° C., igniter(s) 535 can be shut off as external ignition is no longer required to maintain the now self-sustaining exothermic CPOX reaction.

Further in accordance with the present teachings, steam can be introduced into the reformer so that the reformer may be operated to carry out autothermal and/or steam reforming reaction(s).

In one embodiment, the reformer can be initially operated to perform CPOX conversion of a liquid or gaseous reformable fuel thereby providing heat of exotherm that, with or without additional heat, for example, supplied by an electric heater, can be recovered to produce steam in a steam generator. The thus-generated steam can be introduced into the reformer in one or more locations therein. One suitable location is the evaporator where the steam can provide heat to vaporize liquid fuel. For example, steam introduced into wick 515 in reformer 500 illustrated in FIG. 6 can provide heat for vaporizing liquid fuel on wick surfaces at the same time helping to eliminate or suppress clogging of such surfaces.

In another embodiment, a reformer in accordance with the present teachings can be connected to a fuel cell stack in which hydrogen-rich reformate from the reformer is converted to electrical current. Operation of the fuel cell stack, and where present an associated afterburner unit, can provide source(s) of waste heat that can be recovered and utilized for the operation of a steam generator, again, with or without additional heat such as that supplied by an electric heater. The steam from the steam generator can then be introduced into the reformer, for example, through wick 515 of reformer 500 of FIG. 6 , to support autothermal or steam reforming. In this arrangement of integrated reformer and fuel cell stack, the source(s) of waste heat referred to can supply the necessary heat to drive endothermic reaction(s) that are involved in autothermal and steam reforming processes.

FIGS. 8A-8C are diagrams illustrating a start-up procedure of the gas phase chemical reactor in accordance with the present teachings. In FIGS. 8A-8C cold reformer tubes 801 are illustrated in black and hot reformer tubes 802 are illustrated in white. FIGS. 8A-8C illustrate a reactor 410 comprised of 8 rows (4 pairs) of reformer tubes, with a heater 439 associated with each row-pair, i.e., heaters 439 a, 439 b, 439 c and 439 d. During start-up the center reformer tubes will tend to heat up more quickly, as they have thermal input from all directions in the bed and do not have at least one row of the reformer pair exposed to a “cold” reactor wall, i.e., pairs heated by heaters 439 a and 439 d heat up slower than pairs heated by heaters 439 b and 439 c. Heaters 439 a, 439 b, 439 c and 439 d are controlled to achieve a certain reactor bed temperature, and the percentage power to each reformer is then limited and reduced as the reactor reaches its target temperature. However, pairs heated by heaters 439 b and 439 c tend to reach the desired temperature faster than pairs heated by heaters 439 a and 439 d. In order to compensate for this difference in heating times, the power to pairs heated by heaters 439 b and 439 c are preferentially reduce as the desired reactor bed temperature is reached, thus limiting the tendency to overheat the center of the bed (and subsequently damaging the catalyst), while ensuring pairs heated by heaters 439 a and 439 d reach the desired fuel processing temperature (and subsequently reducing coke formation and ensure correct stack operation).

In operation, before initiating a start-up process, the reformer tubes 801 are cold. At start-up as shown in FIG. 8A, igniters 439 a-439 d are all set to at or about their full heating rating. As shown in FIG. 8B, as reformer tubes 802 located more centrally begin to ignite and heat up, the heating rating of all of the igniters 439 a-439 d are reduced, with the inner igniters 439 b and 439 c being reduced at a greater amount than the outer igniters 439 a and 439 d. As shown in FIG. 8C, as all reformer tubes 802 ignite and heat up, the heating rating of all of the igniters 439 a-439 d are further reduced, and eventually to their off state.

It is also understood that the shape of the igniter can vary from the disclosed embodiment. In the above description, the igniter is described and illustrated as having a linear shape, but is not limited to this linear shape. In fact, the igniter can be shaped in any number of configurations to extend along pairs of reformer tubes that are not all aligned along a straight line, but can extend at differing angles or in different planes.

In sum, it should be understood that the delivery systems of the present teachings can deliver the appropriate reactants for carrying out reforming reactions including partial oxidation (“POX”) reforming such as catalytic partial oxidation (“CPOX”) reforming, steam reforming, and autothermal (“AT”) reforming. The liquid reactants such as liquid reformable fuels and water can be delivered from and through the “liquid reformable fuel” delivery components, conduits, and assemblies of the delivery system. The gaseous reactants such as gaseous reformable fuels, steam, and an oxygen-containing gas such as air can be delivered from and through the “gaseous reformable fuel” delivery components, conduits, and assemblies of the delivery system. Certain gaseous reactants such as steam and an oxygen-containing gas can be delivered from and through components and assemblies that are peripheral or secondary to the delivery systems of the present teachings, for example, an oxygen-containing gas can be delivered from a source of oxygen-containing gas that is independently in operable fluid communication with at least one of a vaporizer, a reformer, and a fuel cell stack of a fuel cell unit or system, for example, to mix with a liquid reformable fuel and/or a vaporized liquid reformable fuel prior to reforming.

The present teachings encompass embodiments in other specific forms without departing from the spirit or essential characteristics thereof. The foregoing embodiments are therefore to be considered in all respects illustrative rather than limiting on the present teachings described herein. Scope of the present invention is thus indicated by the appended claims rather than by the foregoing description, and all changes that come within the meaning and range of equivalency of the claims are intended to be embraced therein. 

The invention claimed is:
 1. A multi-tubular chemical reactor comprising: a plurality of spaced-apart reactor units aligned in a single row or parallel rows of essentially identical configuration aligned along a common longitudinal axis corresponding to line L of length X, line L extending from the first to the last reactor disposed within a row, each reactor unit in a row comprising an elongate tube having a wall with internal and external surfaces, an inlet at one end and an outlet at the opposing end, the wall enclosing a gaseous flow passageway at least a portion of which defines a gas phase reaction zone; and at least one igniter for the initiation of a plurality of gas phase exothermic reactions within the gas phase reaction zones of the reactor units, the igniter including a radiant heat-producing element positioned in proximity to, but in physical isolation from, exposed sections of reactor units, the length of such heat-producing element extending from at least about 30 percent up to about 100 percent of length X of line L.
 2. The multi-tubular chemical reactor of claim 1 wherein the multi-tubular chemical reactor is a partial oxidation reformer or autothermal reformer.
 3. The multi-tubular chemical reactor of claim 1 wherein the maximum distance between adjacent reactor units during a steady-state mode of operation is that distance beyond which the temperature of the plurality of spaced-apart reactor units falls below a predetermined minimum array temperature value; and the minimum distance between adjacent reactor units is that distance below which the temperature at an outlet of a reactor unit is greater than a predetermined maximum temperature value.
 4. The multi-tubular chemical reactor of claim 1, further comprising at least one thermocouple disposed within a chamber comprising the plurality of spaced-apart reactor units.
 5. The multi-tubular chemical reactor of claim 1 comprising a plurality of igniters, at least one igniter being disposed at one end of a chamber comprising the plurality of spaced-apart reactor units and at least one igniter being disposed at the opposite end of the chamber.
 6. The multi-tubular chemical reactor of claim 1 comprising a plurality of igniters and a plurality of thermocouples disposed within a chamber comprising the plurality of spaced-apart reactor units, wherein at least one igniter and at least one thermocouple are disposed at one end of the chamber and at least one igniter and at least one thermocouple are disposed at the opposite end of the chamber.
 7. The multi-tubular chemical reactor of claim 6 wherein the plurality of igniters and the plurality of thermocouples are disposed within the chamber such that at least one igniter at one end of the chamber is opposite a thermocouple at the opposite end of the chamber.
 8. The multi-tubular chemical reactor of claim 1 comprising a source of gaseous reactants, the source of gaseous reactants in fluid communication with the gas phase reaction zone(s) of the reactor unit(s).
 9. The multi-tubular chemical reactor of claim 1 comprising a controller for controlling the operation of the multi-tubular chemical reactor, the controller in operative communication with the at least one igniter, and if present, at least one of the at least one thermocouple and the source of gaseous reactants.
 10. A multi-tubular chemical reactor comprising: a plurality of spaced-apart reactor units, each reactor unit comprising an elongate tube having a wall with internal and external surfaces, an inlet at one end and an outlet at the opposing end, the wall enclosing a gaseous flow passageway at least a portion of which defines a gas phase reaction zone; and at least one igniter for the initiation of a plurality of gas phase exothermic reactions within the gas phase reaction zones of the reactor units, the igniter including a radiant heat-producing element positioned in proximity to, but in physical isolation from, exposed sections of reactor units, the length of such heat-producing element extending from at least about 60 percent up to about 100 percent of length X of line L.
 11. The multi-tubular chemical reactor of claim 10 wherein the multi-tubular chemical reactor is a partial oxidation reformer or autothermal reformer.
 12. The multi-tubular chemical reactor of claim 10 wherein the maximum distance between adjacent reactor units during a steady-state mode of operation is that distance beyond which the temperature of the plurality of spaced-apart reactor units falls below a predetermined minimum array temperature value; and the minimum distance between adjacent reactor units is that distance below which the temperature at an outlet of a reactor unit is greater than a predetermined maximum temperature value.
 13. The multi-tubular chemical reactor of claim 10 further comprising at least one thermocouple disposed within a chamber comprising the plurality of spaced-apart reactor units.
 14. The multi-tubular chemical reactor of claim 10 comprising a plurality of igniters, at least one igniter being disposed at one end of a chamber comprising the plurality of spaced-apart reactor units and at least one igniter being disposed at the opposite end of the chamber.
 15. The multi-tubular chemical reactor of claim 10 comprising a plurality of igniters and a plurality of thermocouples disposed within a chamber comprising the plurality of spaced-apart reactor units, wherein at least one igniter and at least one thermocouple are disposed at one end of the chamber and at least one igniter and at least one thermocouple are disposed at the opposite end of the chamber.
 16. The multi-tubular chemical reactor of claim 15 wherein the plurality of igniters and the plurality of thermocouples are disposed within the chamber such that at least one igniter at one end of the chamber is opposite a thermocouple at the opposite end of the chamber.
 17. The multi-tubular chemical reactor of claim 10 comprising a source of gaseous reactants, the source of gaseous reactants in fluid communication with the gas phase reaction zone(s) of the reactor unit(s).
 18. The multi-tubular chemical reactor of claim 10 comprising a controller for controlling the operation of the multi-tubular chemical reactor, the controller in operative communication with the at least one igniter, and if present, at least one of the at least one thermocouple and the source of gaseous reactants.
 19. A method of initiating a gas phase reaction in the chemical reactor of claim 1 having at least 3 igniters, comprising the steps of: initiating maximum heating in all of the igniters; determining initiation of a gas phase exothermic reactions within centrally located reactor units; reducing heating of outer igniters to a first heating level; reducing heating of inner igniters to a second heating level, the second heating level being less than the first heating level; determining initiation of a gas phase exothermic reactions within outer located reactor units; and turning off the heating of the igniters. 